Method and system to prevent carry-over of hydrocarbon mist from an ngl column of an lng plant

ABSTRACT

The present disclosure is directed to a method and system for preventing carry-over of C 2+  hydrocarbon mist from an NGL recovery column in an LNG plant. A wash loop of recirculating liquid hydrocarbon is provided at the upper portion of the NGL column. A sidestream of liquid hydrocarbons collected within the column is removed from the column and pumped to sufficient height to be returned to the column at a temperature substantially equivalent to the temperature of liquid with the upper portion of the column. In one embodiment, liquid hydrocarbons of a desired composition can be loaded and reloaded to a working medium holding drum in fluid communication with the top of the column. The working medium can be selected to be sufficiently heavy not to be lost from the column and to have a suitable freezing point to avoid freezing within the column.

FIELD

The present disclosure relates to methods and systems for operating a natural gas liquids recovery column within a liquefied natural gas plant.

BACKGROUND

In the production of liquefied natural gas (LNG), chilled natural gas is introduced to a natural gas liquids (NGL) recovery column which serves to separate methane to be liquefied from valuable natural gas liquids, i.e., C₂₊ hydrocarbon components to be recovered. The natural gas liquids are removed at the NGL column bottom and are further processed in a series of fractionation columns to recover ethane products, propane products, butane products and C₅₊ products. The NGL column is operated at a lower temperature and higher pressure than the other, aforementioned fractionation columns. When the NGL recovery column is operating relatively close to critical conditions for the fluid at the top of the column, minor fluctuations in the system pressure can result in the formation of NGL mist or fine droplets which can become entrained with the methane leaving the top of the NGL column, a condition referred to as “carry-over.” Demisters in the form of mesh pads are commonly placed at the top of the column to capture such mist, yet such pads alone are sometimes ineffective and the carry-over problem persists. Carry-over results in difficulties in methane liquefaction operations downstream of the NGL column. For instance, the heavier components of the NGL mist may freeze out in the liquefaction operations, resulting in clogging of flow paths.

It is known to provide the NGL recovery column with reflux, in which case the light components leaving the top of the column are condensed in a heat exchanger in which latent heat is removed. The condensed liquid is then separated in a subsequent reflux drum, and returned to the top of the column where the condensed liquid is sprayed into droplets upon which mist is collected and removed from the upward flow of gas. Such reflux operations may reduce carry-over of hydrocarbon mist from the NGL recovery column, at the high energy cost involved in condensing vapor components to liquid components. Furthermore, such operations have been found not to be adequate to control carry-over of hydrocarbon mist under all conditions.

It would be desirable to have a reliable and energy-efficient method for preventing carry-over of hydrocarbon mist from an NGL recovery column in an LNG plant.

SUMMARY

In one aspect, the invention relates to a method for preventing hydrocarbon mist from escaping the top of an NGL recovery column in an LNG plant. The method includes the steps of flowing a hydrocarbon gas stream including a hydrocarbon mist upwardly in an NGL column, spraying droplets of a hydrocarbon liquid into the gas stream to strip at least some of the hydrocarbon mist from the upwardly flowing gas stream, collecting the droplets of the hydrocarbon liquid in a tray within the column, removing a liquid sidestream of the collected hydrocarbon liquid from the column, and returning at least a portion of the liquid sidestream to form the droplets which are sprayed.

In another aspect, the invention relates to a system for preventing hydrocarbon mist from escaping the top of an NGL recovery column in an LNG plant. The system includes a column for recovering NGL. The column includes a natural gas inlet for feeding natural gas to the column, an NGL outlet at a lower portion of the column for dispensing natural gas liquids from the column, a gas outlet at an upper portion of the column for removing gaseous components from the column, at least one tray for collecting liquids within the column, a spray mechanism for generating a spray of droplets which are collected as liquids in the at least one tray, a liquid inlet for receiving and feeding liquid to the spray mechanism and a liquid outlet for receiving liquid from the at least one tray. The system further includes a loop for fluidly connecting the liquid outlet with the liquid inlet to transport a sidestream of liquid, the loop including a pump in fluid communication with the liquid outlet for receiving and pumping the at least a portion of the sidestream to the liquid inlet.

BRIEF DESCRIPTION OF THE DRAWINGS

These and other objects, features and advantages of the present invention will become better understood with regard to the following description, appended claims and accompanying drawings where:

FIG. 1 illustrates a prior art system including a refluxed NGL recovery column and subsequent columns to recover ethane products, propane products, butane products and C₅₊ products.

FIG. 2 illustrates one embodiment of a system to prevent carry-over of hydrocarbon mist from an NGL column.

FIG. 3 illustrates another embodiment of a system to prevent carry-over of hydrocarbon mist from an NGL column.

DETAILED DESCRIPTION

A method is disclosed to prevent the aforementioned problem of carry-over of hydrocarbon mist from the NGL recovery column (also referred to as the NGL column) in an LNG plant, when the NGL column is operated relatively close to critical conditions. By critical conditions is meant the combination of temperature and pressure which creates a thermodynamic condition where the vapor and liquid states cannot be distinguished from each other. The method involves the addition of a wash loop at the column top, in which a suitable hydrocarbon composition is recirculated as a liquid working medium stream in a loop and sprayed at the top of the column in the form of a distributed spray to capture NGL droplets.

Referring to FIG. 1, in a conventional process for producing LNG, chilled natural gas 1 is introduced to a NGL recovery column 10 which separates light components 2 to be liquefied from valuable NGL 3, i.e., C₂₊ hydrocarbon components to be recovered. At least in theory, the light components at the top of the column can be represented by methane, having a critical pressure of 46 bara and critical temperature of −82.6° C. Impurities in the methane tend to enlarge the two-phase region of the fluid phase diagram. The NGL 3 are removed at the NGL column bottom and are further processed in a series of columns to recover ethane products 4 in deethanizer 30, propane products 6 in depropanizer 40 (beginning with C₃₊ products 5), butane products 8 in debutanizer 50 (beginning with C₄₊ products 7) and C₅₊ products 9. Reboiler 20 is also used in conjunction with column 10 to drive fractionation. As shown, the NGL column 10 is refluxed. Light components 2 are sent to heat exchanger 12 where latent heat is removed and C₂₊ vapor components are condensed. Chill stream 13 is sent to reflux drum 14, where methane gas 15 is separated from C₂₊ liquid component stream 16, which is sent to pump 17 and returned to the NGL column 10.

FIG. 2 illustrates the top portion of an NGL column 110 having a wash loop of the present method and system according to one embodiment of the present disclosure. According to the embodiment shown, the wash loop includes the NGL column 110, specifically between spray mechanism 80 and chimney tray 84, sidestream 85 taken from the chimney tray, cross exchanger 76, working medium holding drum 60, pump 66 and heat exchanger 78, as well as optional control elements. The column 110 receives chilled natural gas stream through an inlet (not shown). Methane stream 102 leaves the top of the column for further refrigeration and liquefaction. In the embodiment shown, column 110 has a spray mechanism 80 for distributing liquid working medium within the column near the top of the column. The column also includes a chimney tray 84 therein for collecting liquid 83. The chimney tray 84 includes a chimney 84 a above the inlet (not shown) through which gas flows upwards in the column. The column can also include a series of internal trays 82 (optional). Above the spray mechanism 80 is a mesh pad(s) 90 for capturing NGL droplets which may become entrained in the light components to be removed at the top of the column. NGL components leave the bottom of the column, not shown, for further NGL component recovery.

A sidestream 85 of the liquid collected in the chimney tray 84 is removed from the column through an outlet in the column and heated to a temperature suitable for flashing methane from the stream, e.g. between about −40° C. and −50° C., prior to separation in a working medium holding drum 60. In the embodiment shown, the heating may occur by placing streams 85 (to be heated) and 71 (to be cooled, to be described hereinafter) in a cross exchange relation in cross exchanger 76. Flash valve 88 is used to reduce the stream pressure to facilitate separation of liquid and vapor phases. Methane preferentially accumulates in the vapor phase.

The working medium holding drum 60 functions to receive and hold working medium 55, as well as to separate gaseous components 62 from liquid working medium stream 64. The drum 60 has a liquid inlet for receiving fresh working medium 55, also referred to as makeup hydrocarbon liquid, a gaseous components outlet for releasing gaseous components 62, also referred to as a gas stream including methane, and a liquid working medium stream outlet from which liquid working medium stream 64, also referred to as a methane depleted sidestream, is removed. The working medium 55 can be added as needed (makeup) to the working medium holding drum 60 in fluid communication with the top of the column 110. In alternative embodiments, not shown, makeup hydrocarbon liquid can also be added directly to the liquid sidestream 85 between the column 110 and the working medium holding drum 60 or to the methane depleted sidestream 64. Working medium liquid 55 is added in an amount to maintain sufficient liquid in the circulating loop for spraying droplets in the column. Makeup working medium can be added to the drum 60 as needed to maintain sufficient liquid for a circulating loop, to account for losses over time. After being flashed in the drum 60, the released gaseous components 62 will be directed to other process sections of the plant or recycled to gas streams for further processing. It should be noted that the collected liquid 83 in the chimney tray 84 of the column is not necessarily the same composition as the liquid working medium 55 which is added to working medium holding drum 60, since some light components are dissolved into the working medium due to the high pressure in the column. The majority of the dissolved light components will be flashed out in the drum 60. It is also possible to change the composition of the liquid working medium 55 which is loaded to the drum 60 over time as appropriate, if the feed natural gas composition changes or the operating conditions change. The working medium 55 can be supplied from an external source independent of the LNG system, or it can be diverted from a convenient source within the system. For instance, the working medium 55 can be supplied from a point within NGL column 110 or from one of the other NGL component recovery columns.

The wash loop uses suitable hydrocarbon components or their mixtures as the liquid working medium. The working medium can be selected to be sufficiently heavy not to vaporize and be lost from the top of the column. The working medium can also be selected to have a suitable freezing point to avoid freezing within the column. Freezing temperatures at atmospheric pressure (1.013 bar) for candidate hydrocarbon components are listed in Table 1. In the table, iC_(n) refers to iso-C_(n), and nC_(nrefers) to normal-C_(n).

TABLE 1 Component Freezing T, ° C. C₂ −182.8 C₃ −187.6 iC₄ −159.6 nC₄ −138.3 iC₅ −159.9 nC₅ −129.7 nC₆ −95.3 nC₇ −90.5 nC₈ −56.8 nC₉ −53.5 nC₁₀ −29.7

One of the advantages of the wash loop according to the present disclosure is that it becomes possible to independently control the chemical composition of the working medium in the loop. By having a liquid spray of the working medium in the top of the tower, it is ensured that there will always be a liquid phase present in this section of the tower. The wash loop protects the LNG refrigeration system from excessive loads since there is no phase change within the wash loop as there are in conventional reflux systems. The wash loop can save refrigeration duty when compared with a conventional design in which a reflux stream is created by increasing the column internal vapor and liquid flows. This is because the wash loop only chills a single phase flow (in which gas may be entrained), whereas the conventional design must recondense the additional vapor flow from the column top to generate the reflux stream. Thus the present system is more energy-efficient than a conventional reflux system.

Liquid stream 64 is pumped by pump 66 to a desired flow rate and a sufficient height to be supplied to the top of column 110.

Before the stream is returned to the column 110, it must be cooled. The stream is preferably cooled to a temperature substantially equivalent to the temperature within the upper portion of the NGL column. By “substantially equivalent” is meant as close as practically possible to the temperature in the upper portion of the NGL column, even within a few degrees C., and even within about 3 degree C. of the temperature in the upper portion of the NGL column. Stream 71 enters cross exchanger 76 where cooling of stream 71 occurs by exchanging heat with stream 85. Since the NGL column operates at a low temperature, generally between about −50° C. and −110° C., especially about −90° C., cooled stream 73 may require further cooling in heat exchanger 78 utilizing refrigeration from the LNG plant. Preferably, stream 75 has been cooled to a temperature between about −50° C. and −110° C. before being fed to column 110. Cooled stream 75 can then be fed to column 110 via spray mechanism 80. Stream 75 may contain up to about 3% methane. The spray mechanism can be any suitable liquid distribution mechanism as would be apparent to one skilled in the art.

A flow control system can be implemented for controlling the flow rate at which the working medium stream is returned to the column 110. The flow control system includes a controller 70 for controlling the flow rate. The controller 70 is in communication with a liquid level detector 72 for measuring the liquid level in the chimney tray 84. If the level becomes low, the control system is reset, and controller 70 operates valve 74 to resupply fluid to the desired level. Flow meter 68, also in communication with controller 70, measures the flow rate of stream 67. If the rate becomes lower or higher than control limits, the controller 70 operates valve 74 to increase or decrease the rate, respectively.

An alternative embodiment is shown in FIG. 3. According to this embodiment, the wash loop includes the NGL column 110 (equivalent to the NGL column 110 shown in FIG. 2), specifically between spray mechanism 80 and chimney tray 84, sidestream 85 taken from the chimney tray, pump 66 and heat exchanger 78, as well as optional control elements. In this embodiment, sidestream 85 is pumped by pump 66 to sufficient height to be returned to the top of column 110. The pump suction head 65 of line 85 can be set to an appropriate height to avoid possible operational difficulties as would be apparent to one skilled in the art. Stream 86 coming from pump 66 can be augmented by stream 98 representing additional or makeup working medium. The addition of stream 98 can be controlled by a controller 92 in communication with a level detector 72 for detecting the level of liquid in the chimney tray 84. When the level of liquid is sufficiently low, controller 92 opens valve 96 on makeup working medium line 94. Stream 86 can flow through a flowmeter 68, which is in communication with a controller 70 for controlling valve 74. Stream 77 is chilled in exchanger 78 as described above prior to returning the liquid stream to the column 110 as stream 75.

Where permitted, all publications, patents and patent applications cited in this application are herein incorporated by reference in their entirety, to the extent such disclosure is not inconsistent with the present invention.

Unless otherwise specified, the recitation of a genus of elements, materials or other components, from which an individual component or mixture of components can be selected, is intended to include all possible sub-generic combinations of the listed components and mixtures thereof. Also, “comprise,” “include” and its variants, are intended to be non-limiting, such that recitation of items in a list is not to the exclusion of other like items that may also be useful in the materials, compositions, methods and systems of this invention.

From the above description, those skilled in the art will perceive improvements, changes and modifications, which are intended to be covered by the appended claims. 

1. A method for reducing hydrocarbon mist from escaping the top of an NGL recovery column in an LNG plant, the method comprising: a. flowing a hydrocarbon gas stream including a hydrocarbon mist upwardly in an NGL column; b. spraying droplets of a hydrocarbon liquid into the gas stream to strip at least some of the hydrocarbon mist from the upwardly flowing gas stream; c. collecting the droplets of the hydrocarbon liquid in a tray within the column; d. removing a liquid sidestream of the collected hydrocarbon liquid from the column; and e. returning at least a portion of the liquid sidestream to form the droplets which are sprayed in step b.
 2. The method of claim 1, wherein the at least a portion of the liquid sidestream does not change phase when returned to form the droplets.
 3. The method of claim 1, further comprising cooling the at least a portion of the liquid sidestream to a temperature substantially equivalent to the temperature within an upper portion of the column prior to returning the at least a portion of the liquid sidestream to the column.
 4. The method of claim 1, further comprising supplying the liquid sidestream to a working medium holding drum in which the liquid sidestream is separated into a methane depleted sidestream and a gas stream including methane.
 5. The method of claim 4, wherein the liquid sidestream is heated prior to supplying the liquid sidestream to the working medium holding drum.
 6. The method of claim 4, further comprising adding a makeup hydrocarbon liquid to at least one of the liquid sidestream, the methane depleted sidestream or the working medium holding drum so that the methane depleted sidestream is of a predetermined composition.
 7. The method of claim 2, wherein the at least a portion of the liquid sidestream is cooled such that the droplets that are sprayed are at a temperature of between about −50° C. and −110° C.
 8. The method of claim 6, wherein the makeup hydrocarbon liquid is added to the working medium holding drum as needed to maintain sufficient liquid for spraying droplets in the column.
 9. The method of claim 5, further comprising cooling the at least a portion of the liquid sidestream to a temperature substantially equivalent to the temperature within an upper portion of the column prior to feeding the at least a portion of the liquid sidestream to the column, wherein the cooling of the at least a portion of the liquid sidestream is conducted in cross exchange with the heating of the liquid sidestream prior to supplying the liquid sidestream to the working medium holding drum.
 10. The method of claim 9, further comprising subjecting the at least a portion of the liquid sidestream to further cooling prior to being returned to the column.
 11. The method of claim 6, wherein the makeup hydrocarbon liquid comprises C₂₋₁₀ hydrocarbons having a freezing temperature between about −182.8° C. and about −29.7° C.
 12. A system for preventing hydrocarbon mist from escaping the top of an NGL recovery column in an LNG plant, comprising: a. a column for recovering NGL, the column comprising: i. a natural gas inlet for feeding natural gas to the column; ii. an NGL outlet at a lower portion of the column for dispensing natural gas liquids from the column; iii. a gas outlet at an upper portion of the column for removing gaseous components from the column; iv. at least one tray for collecting liquids within the column; v. a spray mechanism for generating a spray of droplets which are collected as liquids in the at least one tray; vi. a liquid inlet for receiving and feeding liquid to the spray mechanism; vii. a liquid outlet for receiving liquid from the at least one tray; and b. a loop for fluidly connecting the liquid outlet with the liquid inlet to transport a sidestream of liquid, the loop including a pump in fluid communication with the liquid outlet for receiving and pumping the at least a portion of the sidestream to the liquid inlet.
 13. The system of claim 12, wherein the loop comprises: a heat exchanger in fluid communication with the pump for cooling the at least a portion of the sidestream.
 14. The system of claim 12, further comprising: a working medium holding drum in fluid communication receiving the at least a portion of the sidestream which separates the at least a portion of the sidestream into a methane depleted sidestream and a gas stream including methane, the methane depleted sidestream being pumped by the pump to the liquids inlet.
 15. The system of claim 12, further comprising: a. a controller for controlling the flow rate of the at least a portion of the sidestream; b. a valve in communication with the controller for increasing or decreasing the flow rate of the at least a portion of the sidestream; c. a flow meter in communication with the controller for measuring the flow rate of the at least a portion of the sidestream; and d. a liquid level detector in communication with the controller for measuring the liquid level in the tray. 